Production of cleaned and cooled synthesis gas

ABSTRACT

The hot raw synthesis gas stream leaving the reaction zone of a free flow partial oxidation gas generator at a temperature in the range of about 1800° to 3000° F. is passed through a first gas diversion and residue separation zone where the velocity of the gas stream is reduced and its direction is diverted into a side transfer line. Solid material and molten slag separate by gravity from the gas stream. The hot gas stream is then introduced into a second gas diversion and residue separation zone where additional residue is separated. About 0.5 to 20 vol. % of the hot gas stream may be passed through bottom outlets in said first and second gas diversion zones in order to prevent bridging. The hot gas stream from the second gas diversion zone is passed upwardly through a radiant cooler where additional solid matter is removed by gravity and the gas temperature is reduced to a temperature in the range of about 900° to 1800° F. In one embodiment, the second diversion and residue separation zone is a thermally insulated cyclone. By the subject process, 70 to 95 wt. % of the combustion residue is removed from the raw stream of synthesis gas, and the temperature of the gas stream is reduced below the maximum safe operating temperature for downstream devices used to recover energy from the hot gas stream, such as a conventional convection type gas cooler.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates to the manufacture of cleaned and cooled gaseous mixtures comprising H₂ and CO. More particularly it pertains to the process for producing a cleaned and cooled stream of synthesis gas, fuel gas, or reducing gas by the partial oxidation of ash containing solid carbonaceous fuels.

2. Description of the Prior Art

Various amounts of molten slag and solid matter such as soot and ash are contained in the hot raw gas stream leaving a partial oxidation generator in which solid hydrocarbonaceous fuels such as coal are reacted with steam and free oxygen to produce gaseous mixtures comprising carbon monoxide and hydrogen. The life of such equipment as gas coolers, compressors, and turbines that are contacted downstream by the hot raw gas stream, may be increased by removing entrained solids from the gas stream. Solids removal from a raw synthesis gas stream will prevent plugging of catalyst beds. Further, environmentally acceptable fuel gas may be produced.

In co-assigned U.S. Pat. No. 2,871,114-Du Bois Eastman, the hot raw gas stream leaving the gas generator is passed first through a slag pot and then into a water quench tank. Not only is the raw gas stream leaving the quench tank saturated with water, but all of the sensible heat in the gas stream is dissipated in the quench water at a comparatively low temperature level. In U.S. Pat. No. 4,054,424 no means is provided for removal of the slag from the system. This differs from the subject invention by which entrained residue from the partial oxidation process is removed from the raw synthesis gas without quenching all of the hot raw gas stream in water or other coolant.

SUMMARY

This invention pertains to a process for the partial oxidation of the ash containing solid carbonaceous fuel, such as coal, for producing a cleaned and partially cooled stream of synthesis gas, fuel gas, or reducing gas. A solid carbonaceous fuel is reacted with a free-oxygen containing gas, with or without a temperature moderator, in a down-flow refractory lined noncatalytic free-flow gas generator at a temperature in the range of about 1800° to 3000° F. and a pressure in the range of about 10 to 190 atmospheres to produce a raw gas stream comprising H₂, CO, CO₂, and one or more materials from the group H₂ O, H₂ S, COS, CH₄, NH₃, N₂, A, and containing molten ash and particulate matter. Most of the combustion residue entrained in the hot raw gas stream leaving the reaction zone is removed and the temperature of the raw gas stream is reduced to a temperature in the range of about 900° to 1800° F. by means of the subject process. By this means fouling of the tubes of a downstream convection type waste heat boiler may be avoided. Further, the life of such downstream equipment as compressors and turbines may be increased. Removing entrained solids from the raw synthesis gas stream will prevent plugging of downstream catalyst beds. Removal of the entrained solids from the hot raw gas stream mainly takes place in two separate gas diversion and residue separation zone. The gas stream is then passed upwardly through the central unobstructed vertical passage of a vertical tube-wall cooled radiation section where additional solid matter is removed by gravity and the temperature of the gas stream is reduced. In one embodiment of the process, the second gas diversion and residue separation zone comprises one or more cyclone separators. In still another embodiment, the second gas diversion and solid separation zone comprises an impingement separator.

The subject process is carried out in two separate vertical pressure vessels. The upper portion of the first vessel contains the refractory lined reaction zone of the gas generator which is directly connected at the bottom to the first gas diversion and residue separation zone. Solid residue and slag entrained in the gas stream passes through an outlet in the bottom of the first diversion chamber and drops by gravity into a pool of water contained in the bottom of the first vessel. Optionally, a comparatively small stream of bleed gas passes through the bottom outlet in the first diversion chamber and is removed from the vessel. This stream of hot gas prevents bridging of said bottom outlet with solid matter. The second vertical vessel is located close to and parallel to the first vertical vessel. The upper portion of the second vertical vessel consists of a tube-wall cooled radiant section. The second gas diversion and residue separation zone is located directly beneath the upper radiant cooling section, and is connected to the first diversion zone by way of a transfer line. Solids separated in the second diversion zone drop by gravity through an outlet in the bottom of the second diversion chamber and into a pool of water contained in the bottom of the second vessel. In a preferred embodiment, the hot water containing solids removed from the bottoms of the two vessels is passed in indirect heat exchange with boiler feed water. By this means the boiler feed water is preheated before it is introduced into the tube wall of the radiant cooling section as a portion of the coolant.

BRIEF DESCRIPTION OF THE DRAWING

The invention will be further understood by reference to the accompanying drawing in which:

FIG. 1 is a schematic drawing which shows the subject process in detail.

FIG. 2 is a schematic drawing which shows an embodiment of the subject process in which the second gas diversion and solids separation chamber consists of a cyclone.

DESCRIPTION OF THE INVENTION

The present invention pertains to an improved continuous process and related apparatus for cleaning and cooling a hot raw gas stream from a free flow non-catalytic partial oxidation gas generator. The hot raw gas stream principally comprises H₂, CO, CO₂, and one or more materials from the group H₂ O, H₂ S, COS, CH₄, NH₃, N₂, A, and containing entrained solid matter and molten ash. The hot raw gas stream is made by the partial oxidation of an ash containing solid carbonaceous fuel, such as coal i.e. anthracite, bituminous, sub-bituminous, or lignite. One ton of coal contains the same amount of energy as three to four barrels of crude oil. Accordingly, coal is the most promising material to replace the dwindling world-wide oil and natural reserves. One third of the world's economically recoverable coal reserves are located in the U.S. There is enough coal in the U.S. to last more than 200 years.

Ground solid fuel is introduced into the gas generator either alone or in the presence of a substantially thermally liquifiable or vaporizable hydrocarbon or carbonaceous material and/or water, or entrained in a gaseous medium such as steam, CO₂, N₂, recycle synthesis gas, and air. Vaporizable hydrocarbons include by definition petroleum distillates and residue, oil derived from coal, shale oil, crude petroleum, gas oil, tar sand oil, cycle gas oil from fluid-catalytic cracking operation, furfural extract of coker gas oil, and mixtures thereof. Solid carbonaceous fuelincludes by definition particulate carbon, coal, coke from coal, lignite, petroleum coke, oil shale, tar sands, asphalt, pitch and mixtures thereof.

By means of the subject invention the combustion residues entrained in the raw gas stream from the reaction zone of the gas generator may be reduced to an acceptable level of concentration and particle size so that the hot gas stream may be used in downstream heat exchange equipment, or in other devices which utilize the energy contained in the hot gas stream. The recovery of thermal energy from the raw gas stream leaving the reaction zone of the partial oxidation gas generator is made difficult by the presence in the generator exhaust gases of combustion residues including particulate solids and droplets of molten slag which result from the fusion of the ash content of the coal fed to the gas generator. The concentration of solids in the hot raw gas stream may be in the range of about 0.1 to 4 grams per standard cubic foot (SCF). The particle size may be in the range of about 40 to 1000 micrometers or larger. Unless removed, slag and particulate matter entrained in the hot gas stream, will deposit out and foul heat exchange surfaces. The thermal efficiency of the process will be thereby impaired.

By the instant invention, the molten slag droplets are solidified and removed along with other particulate solid matter before they encounter the surfaces of conventional energy utilizing means such as expansion and gas turbines, and heat exchangers i.e. convectional-type gas coolers. For example, the gas cooler described in U.S. Pat. No. 3,690,774 with helical or spiral coiled tubes may be used to further cool the partially cooled and cleaned synthesis gas, as produced by our process. Boilers of this general design have a high heat exchange surface. However, the coils have sharp bends which make the tubes vulnerable to plugging. The coils are difficult to remove and replace, and they are expensive to clean and maintain. Further, for metallurgical reasons, the maximum inlet gas temperature should be held to a safe operating temperature in the range of about 900° F. to 1800° F. These difficulties are overcome by the subject invention which reduces the temperature of the hot raw gas stream coming from the reaction zone of the gas generator and also removes entrained solids and slag. The thermal efficiency of the partial oxidation gasification process is thereby increased by recovering energy from the hot raw gas stream. Further, more by-product steam for use in the process or for exporting may be produced by indirect heat exchange of the hot gas stream with water, first in the radiant cooler, and second in the convection type gas cooler. By means of the subject invention, the recovery of thermal energy from the hot gases is simplified.

A typical partial oxidation synthesis gas generator is shown in co-assigned U.S. Pat. No. 2,818,326. A burner is located in the top of the gas generator along the central vertical axis for introducing the feed streams. A suitable annulus-type burner is shown in co-assigned U.S. Pat. No. 2,928,460. The gas generator is a vertical cylindrical steel pressure vessel lined on the inside with a thermal refractory material.

The solid carbonaceous fuels are preferably ground to a particle size so that 100% of the material passes through an ASTM E 11-70 Sieve Designation Standard 425 μm (Alternative No. 40) and at least 40% passes through an ASTM E 11-70 Sieve Designation Standard 75 μm (Alternative No. 200). 1000 μm=1 mm. The ground solid carbonaceous fuel is then introduced into a storage hopper at room temperature and atmospheric pressure.

The normal moisture content of the solid carbonaceous fuels as received at the point of use can vary in the range of about 0 to 40 weight percent. For example, the moisture content as received for anthracite and bituminous coals may be in the range of about 2 to 10 wt. % of dry weight, up to 30 wt. % of dry weight for sub-bituminous coals, and up to 40 wt. % of dry weight, or more for lignite. Generally, the solid carbonaceous fuel may be used without reducing the moisture content as received. However, predrying may be required in some instances to reach a more desirable moisture content, say below 20 wt. % or even below 2.0 wt. %.

The ground solid carbonaceous fuel in the form of a slurry with water or liquid hydrocarbon, or entrained in a gaseous medium as previously described, is passed into the reaction zone of the partial oxidation gas generator by way of one of the passages in the annulus-type burner. This feedstream may be at room temperature or it may be preheated to a temperature up to as high as about 600°, but preferably below the cracking temperature. Advantageously, the carbonaceous feed may be preheated by direct or indirect heat exchange with by-product superheated or saturated steam, or advantageously by other suitable means to be described later.

A supplemental temperature moderator to moderate the temperature in the reaction zone may not be required with water slurries and when the solid fuel is dispersed in some gaseous hydrocarbon fuels. Suitable temperature moderators include superheated steam, saturated steam, unsaturated steam, water, CO₂ -rich gas, a portion of the cooled exhaust from a turbine employed downstream in the process, nitrogen in air, by-product nitrogen from a conventional air separation unit, and mixtures of the aforesaid temperature moderators. The temperature moderator may be introduced in admixture with either or both reactant streams. Alternatively, the temperature moderator may be introduced into the reaction zone of the gas generator by way of a separate conduit in the fuel burner.

The term free-oxygen containing gas, as used herein is intended to include air, oxygen-enriched air, i.e. greater than 21 mole % oxygen, and substantially pure oxygen, i.e. greater than 95 mole % oxygen, (the remainder comprising N₂ and rare gases). Free-oxygen containing gas may be introduced into the burner at a temperature in the range of about ambient to 1,800° F.

The relative proportions of solid carbonaceous fuel, temperature moderator, and free-oxygen in the reaction zone of the gas generator are such as to ensure an autogenous temperature in the gas generation zone within the range of about 1800° to 3000° F., such as about 2000° to 2800° F., and to produce a particulate phase containing ash and about 0.1 to 20 wt. % of the organic carbon in the feed, and typically about 1 to 4 wt. %. The particulate phase is entrained in the effluent gas stream leaving the reaction zone along with any non-combustible slag.

Other operating conditions in the gas generator include; pressure in the range of about 10 to 190 atmospheres and preferably about 30 to 100 atmospheres; the ratio of the atoms and free-oxygen containing gas plus the atoms of organically combined oxygen in the solid carbonaceous fuel per atom of carbon in the solid carbonaceous fuel (O/C atomic ratio) may be in the overall range of about 0.7 to 1.6. More specifically, with substantially pure oxygen feed to the reaction zone the broad range of said O/C atomic ratio may be about 0.7 to 1.5 and preferably with air feed to the reaction zone the broad range may be about 0.8 to 1.6 and preferably about 0.9 to 1.4. With H₂ O as the temperature moderator, the weight ratio of H₂ O to carbon in the solid carbonaceous fuel feed is in the range of about 0.5 to 2.0 and preferably in the range of about 0.7 to 1.0. With substantially pure oxygen feed to the gas generator, the composition of the effluent gas from the gas generator in mole % dry basis may be as follows: H₂ 5 to 40, CO 40 to 60, CO₂ 5 to 25, CH₄ 0.01 to 3, and H₂ S+ COS 0 to 5, N₂ nil to 5, and A nil to 1.5. With air feed to the gas generator, the composition of the generator effluent gas in mole % dry basis may be as follows: H₂ 2 to 20, CO 15 to 35, CO₂ 5 to 25, CH₄ 0 to 2, H₂ S+COS 0 to 3, N₂ 45 to 70, and A 0.1 to 1.5.

The hot raw gas stream produced in the reaction zone, leaves the reaction zone by way of a centrally located outlet in the bottom of the reaction zone which is coaxial with the central longitudinal axis of the gas generator. The hot gas stream passes through said bottom outlet and expands directly into a gas diversion and residue separation chamber which is preferably located directly below the reaction zone. The gas diversion and residue separation zone is refractory lined and is preferably coaxial with the central vertical axis of the reaction zone of the gas generator. Preferably, both zones are within the same upright closed pressure vessel. Alternately, the diversion chamber may be in a separate vessel attached to the bottom outlet of the gas generator. The residence time in the reaction zone of the gas generator is in the range of about 1 to 10 seconds, say about 3 to 5 seconds. The net internal volume of the first gas diversion and residue separation chamber is only about 5 to 50% of the net internal volume of the reaction zone.

The hot raw gas stream passes through the bottom outlet in the reaction zone at a velocity in the range of about 20 to 50 ft. per sec., say about 30 to 40 ft. per sec. The velocity of the hot gas stream is reduced in the gas diversion chamber and particulate matter and molten slag drop out of the gas stream by gravity. This solid matter and molten slag moves by gravity through an outlet located at the bottom of the diversion chamber and preferably, into a pool of water contained in a slag chamber located below. Preferably, the inlet and bottom outlets of the diversion chamber are centrally located and coaxial with the central vertical axis of the diversion chamber. Preferably, the slag chamber is located directly below the bottom outlet of the diversion chamber, and in the same pressure vessel as the reaction zone and the diversion chamber. Preferably, the central vertical axis of the slag chamber is coaxial with that of the gas diversion chamber. Alternately, the slag chamber may be in a separate vessel which is attached to the bottom of the vessel containing the diversion chamber. In one embodiment, the slag chamber is lined with refractory and operated dry.

The shape of the gas diversion chamber may be cylindrical, spherical, or it may be outwardly diverging or expanding conically from the entrance to an enlarged central portion followed by an inwardly converging or converging conically shaped portions to separate outlets in the side and bottom. An outlet located in the side wall of the slag chamber below the bottom exit in the diversion chamber but above the water level, and a cooled control valve, may be used optionally for withdrawing a comparatively small bleed stream of raw hot gas from the slag chamber. The bleed gas stream enters the slag chamber by way of the bottom outlet in the gas diversion chamber carrying with it entrained particulate matter and molten slag. The later material drops to the bottom of the slag chamber. When necessary, this bleed stream will keep the bottom outlet in the diversion chamber hot, thereby preventing bridging and plugging with solid matter and slag. From about 0 to 20 vol. %, say about 0.5 to 10 vol. % and typically 5 vol. % of the hot raw gas stream entering the first gas diversion chamber may be employed as bleed gas. The bleed gas leaving the slag quench chamber by way of said side outlet and control valve is preferably passed through a separate heat exchanger. For example, the hot bleed gas may be used to preheat a coalwater slurry feedstream to the gas generator. The bleed gas may be then mixed with the main gas stream leaving a conventional convection-type gas cooler. Alternately, the stream of bleed gas may be used as the transport medium for powdered solid carbonaceous fuel and introduced into the gas generator with the feed.

From about 80.0 to 100 vol. % of the hot raw gas stream entering the first gas diversion chamber leaves by way of a thermally insulated side transfer line and passes directly into the inlet of a second gas diversion and residue separation zone, which is located nearby in a separate vertical cylindrical pressure vessel. The second pressure vessel is parallel to the first pressure vessel and closely connected thereto by said transfer line. In a preferred embodiment, the gas diversion and residue separation zone in the second vessel is sized larger but is similar in shape and design to the gas diversion and residue separation chamber previously described in the first vessel. The central vertical axis of said gas diversion and residue separation zone is preferably coaxial with the central vertical axis of the second vessel. The net internal volume for the gas diversion chamber in the second vessel is about 4 to 10 times greater than the net internal volume for the gas diversion chamber in the first vessel. Additional particulate solids and slag drop out of the gas stream by gravity in the second gas diversion vessel and fall through a central opening in the bottom of the gas diversion chamber into a pool of water contained in the slag chamber located in the bottom of the second vessel. Preferably, the central vertical axis of the gas diversion and residue separation chamber in the second vessel is coaxial with the central vertical axis of the slag chamber. A bleed stream comprising about 0 to 20 vol. %, say about 0.5 to 5 vol. % of the gas stream entering the second gas diversion zone, is optionally passed through the bottom opening in the diversion chamber and then through an outlet in the wall of the slag chamber located above the pool of water contained in the bottom. The function and disposition of this second bleed stream is similar to that of the first bleed stream described previously in connection with the slag chamber in the first vessel. In one embodiment, the slag chamber in the second vessel is lined with refractory and operated dry.

The longitudinal axis of the transfer line connecting the first and second gas diversion and residue separation chambers is preferably in the same plane with the central vertical axes of the two vessels. Further, the longitudinal axis of the transfer line makes an angle with and measured clockwise starting in the third quadrant from the central vertical axis of the second gas diversion and residue separation zone in the range of about 30° to 120°. Suitably, this angle may be in the range of about 40° to 110°, say about 60°, and preferably upward or downward. The actual angle is a function of such factors as temperature and velocity of the gas stream, and the composition, concentration and characteristics of the entrained matter to be removed. For example, when the raw gas stream contains liquid slag of high fluidity, the longitudinal axis of the raw inlet nozzle may be pointed upward at an angle of about 60° measured clockwise from the central vertical axis of the second vessel starting in the third quadrant. Much of the slag would run down the transfer line into the first gas diversion chamber and from there into the pool of water located at the bottom of the first vessel. On the other hand, when the liquid slag is viscous, the flow of the slag may be helped along by pointing the transfer line downward say at an angle of about 120° measured clockwise from the central vertical axis of the second vessel starting in the third quadrant. The high velocity of the hot raw gas stream passing through the transfer line and the force of gravity would then help to move the viscous liquid slag into the second gas diversion chamber, where the slag may be separated from the gas stream by gravity. The velocity of the hot raw gas stream through the transfer line is in the range of about 20 to 100 ft. per sec., say about 30 to 60 ft. per sec., and typically about 40 ft. per sec. The reduced velocity of the hot raw gas stream passing upwardly through the second gas diversion chamber located in the second upright closed pressure vessel permits the entrained solid materials to fall by gravity down through the central opening in the bottom of the second gas diversion chamber into the pool of water contained in the bottom of the second vessel. Optionally, in place of a thermal refractory lining, the inside walls of one or both of the slag catch pots at the bottom of the first and second vessels may be water jacketed or water cooled walls. The velocity of the hot raw gas stream through the transfer line is in the range of about 1.5 to 3 times the velocity of the hot raw gas stream passing through the bottom outlet of the reaction zone.

The main hot raw gas stream passing upwardly through the second gas diversion chamber leaves by way of a central outlet in the top at a velocity in the range of about 1 to 10 ft. per sec., and at a temperature in the range of about 1800° F. to 3000° F. Very little, if any, of the sensible heat in the hot raw gas stream is lost during its passage through the first and second gas diversion and residue separating zones. The hot raw gas stream then directly enters into the bottom of a radiant cooling section located in the upper portion of the second pressure vessel and freely passes upwardly through the central unobstructed vertical passage on the inside of a water-cooled tube-wall. Preferably, the central vertical axis of the radiant cooling section is coaxial with the central vertical axis of the second pressure vessel. The net internal volume of the radiant cooling section is about 5 to 10 times the net internal volume of the reaction zone of the gas generator. Upright tubes, through which a coolant passes, line the inside walls of the radiant cooling section. The walls of the pressure vessel are thereby protected from thermal and corrosive damage. The dwell time of the gases passing up through the radiant cooling section is in the range of about 15 to 50 seconds, say 20 to 40 seconds. The vertical radiant cooling section being located immediately upstream of an energy utilizing means provides an additional chamber for the gravity settling and separation of solid particles and slag from the hot gas stream, thereby protecting the energy utilizing means from being fouled. One further function of the radiant cooling section is to cool the upflowing hot gas stream to below the maximum safe operating temperature for the energy utilizing means that follows i.e. to a temperature of about 900° F. to 1800° F. Also, during this gas cooling period at least the outer shell of any remaining ash particles in the gas stream is solidified. This prevents the particles from sticking to the tubes in the radiant and convection sections of the gas coolers.

For example, the hot gas stream first gives up a part of its heat to the boiler tubes located in the radiant cooling section. Then the gas with a reduced temperature passes into a convection zone likewise equipped with boiler tubes where it is further cooled to a temperature in the range of about 650° to 150° F. The walls of the vertical steel pressure vessel containing the radiant cooling section are protected against the action of the upwardly flowing hot gases by the cooling surfaces of the tube-wall placed in front of the vessel wall. In a preferred embodiment, a plurality of thin-walled vertical tubes with or without side fins line the inside walls of the radiant cooling section of the second vessel. The adjacent rows of tubes are longitudinally welded together to make an annular gas-tight wall of tubes. The lower and upper ends of each of said tubes may be respectively connected to lower and upper annular shaped headers. When the coolant in the radiant cooler is water or a mixture of water and steam, the highest temperature that the pressure shell can reach is the temperature of the saturated steam within the radiant cooler. Boiler feed water is introduced into the bottom header and then passes up through the plurality of separate upright tubes into the top header. The mixture of steam and water is removed from the top header and introduced into an external steam drum where separation takes place. The saturated steam removed from the steam drum may be used elsewhere in the process to provide heat or power. Optionally, at least a portion of the saturated steam may be superheated. The hot water separated in the steam drum may be returned to the bottom header of the radiant cooler.

Water containing solids and slag in the slag chambers located at the bottom of vessels 1 and 2 is removed by way of a conventional lockhopper and sent to a solids removal zone. The reclaimed quench water may be then recycled back to the slag chambers at the bottom of vessels 1 and 2. In a preferred embodiment, the quench water containing solids leaving the slag chambers in vessels 1 and 2 at a temperature in the range of about 400° to 550° F. is passed in indirect heat exchange with boiler feed water. By this means, the temperature of the boiler feed water is increased about 10° to 100° F. The preheated boiler feed water is then introduced into the bottom header of the radiant cooler.

In one embodiment of the subject invention the slag chamber in vessel 1, vessel 2, or both vessels is equipped with a conventional dip tube. In such case, the solid material and slag and optionally bleed gas may be passed through the bottom outlet in one or both of the separate gas diversion and residue separation chambers located in each pressure vessel, and then passed through respective dip tubes that terminate below the level of the water contained in the respective slag chambers. By this means, the bleed gas may be cleaned and partially cooled.

In another embodiment of the subject invention, the gas diversion and residue separation means in the second pressure vessel is replaced by a single-stage or multiple-stage cyclone, and alternatively with an impingement separator. In this embodiment, both wet and dry type slag pots may be employed to receive the solid matter and slag separated from above. The cyclone is thermally insulated to prevent heat loss from the hot gas stream passing through. The cyclone is essentially a separating chamber in which the force of gravity is replaced by centrifugal acceleration. The raw gas stream leaving the first gas diversion and residue separating chamber in the first vessel and containing particulate solids and slag passes through the transfer line and enters the cylindrical conical chamber of the cyclone tangentially at one or more entrances at the upper end. The gas path involves a double vortex with the raw gas stream spiraling downward at the outside and the clean gas stream spiraling upward on the inside to a plenum at the top. The clean gas stream leaves by way of a central outlet along the vertical axis at the top of the cyclone and then passes upward directly into the bottom of a vertical free-flow radiant cooling section of vessel 2. The solid particles, by virtue of their inertia, will tend to move in the cyclone towards the separator wall from which they are led into a bottom central outlet and discharge pipe. Small size particles will form clusters that drop into the pool of water contained in the slag chamber at the bottom of vessel 2. About 0 to 20 vol. %, such as about 0.5 to 10 vol. %, say 5 vol. % of the hot gas stream may by-pass the cyclone inlet and exit by way of the dust trap and bottom outlet along with the solid matter and slag. This will keep the bottom outlet hot and prevent bridging. In such case, the bleed stream leaves the vessel by way of an insulated side outlet located above the pool of water at the bottom of the slag chamber. The hot stream of bleed gas then passes through an insulated line and cooled control valve. In one embodiment a plurality of single stage cyclones are employed. Each cyclone discharges into a common plenum chamber. The gas stream leaving the outlet in the plenum chamber enters directly into the radiant cooling section. In another embodiment, at least one multiple-stage cyclone unit is employed. In such case, the partially cleaned gas stream that is discharged from the first-stage cyclone is passed into the inlet to a second-stage cyclone. The clean gas stream from each second-stage cyclone is discharged into a common plenum chamber, and from there into the tube-wall cooled radiation section. In still another embodiment, the second gas diversion and residue separation chamber is replaced by a conventional impingement gas-solids separator. For a more detailed discussion of cyclone and impingement separators, reference is made to CHEMICAL ENGINEERS HANDBOOK-Perry and Chilton, Fifth Edition 1973 McGraw-Hill Book Co. Pages 20-80 to 20-87 which is incorporated herewith by reference.

Thus, advantageously, by the subject process the temperature of the hot raw gas stream leaving the partial oxidation gas generator may be reduced to below the safe maximum operating temperature of a downstream convection-type gas cooler. Further, about 70 to 95 wt % of entrained solid matter and slag are removed from the hot gas stream. Fouling of heat exchange surfaces, catalyst beds, and other equipment which may be contacted by the hot gas stream is thereby prevented. No liquid scrubbing fluid is employed. Accordingly, the sensible heat in the hot gas stream is not wasted by vaporizing scrubbing fluid, which may then contaminate the gas stream. By-product saturated or super heated steam is produced. This steam may be used elsewhere in the process or exported. For example, steam may be used for heating purposes, for producing power in a steam turbine, or recycled to the gas generator as a temperature moderator. Alternately, at least a portion of the cleaned and cooled gas stream leaving the radiant cooling section may be passed through an expansion turbine for the production of mechanical energy, electrical energy, or both. The gas stream leaving the downstream convection-type gas cooler at a temperature in the range of about 150° to 600° F., or exiting from some other energy utilizing means, optionally may be subjected to additional process steps including gas scrubbing, purification, or both, depending on its intended use as a synthesis gas, reducing gas, or fuel gas.

DESCRIPTION OF THE DRAWING

A more complete understanding of the invention may be had by reference to the accompanying drawing which illustrates in FIGS. 1 and 2, two embodiments of the invention.

In FIG. 1, closed cylindrical vertical steel pressure vessel 1 comprises three main sections: reaction zone 2 lined with refractory 3 in the upper portion, gas diversion and residue separation chamber 4 which is located below reaction zone 2 and connected by passage 5, and slag chamber 6 which contains of a pool of water 31 at the bottom of pressure vessel 1. Alternately, the previously described three sections may be contained in three separate pressure vessels which are vertically stacked, connected, communicating, and arranged in a manner similar to that shown in FIG. 1.

Top outlet 7 is located in the top and bottom outlet 8 is located in the bottom of vessel 1. The axes of outlets 7 and 8 lie along the central vertical axis of vessel 1. Annulus-type burner 9, comprising center passage 10, inlet 11, and annulus passage 12 is mounted in upper outlet 7. A mixture of ground coal in a transport medium (such as a coal-water slurry) in line 13 is pumped by means of pump 14 through line 15 into heat exchanger 16 where the slurry is preheated by indirect heat exchange with at least a portion of the bleed gas from lines 17, 18, or both. The preheated coal-water slurry in line 19 is passed through inlet 11 and annulus passage 12 of burner 9 into reaction zone 2 where it impinges and reacts by partial oxidation with a stream of free-oxygen containing gas. For example, a stream of substantially pure oxygen or air in line 20 is preheated in heat exchanger 21 with steam from line 22. The preheated free-oxygen containing gas is then passed through line 23 and center passage 10 of burner 9 into the reaction zone where the partial oxidation reaction takes place with the coal-water slurry. The cooled bleed stream leaving the heat exchanger 16 by way of line 24 is mixed downstream in the process with the cooled main gas stream leaving a convection type of gas cooler (not shown). Alternately, the heating fluid in heat exchanger 16 may be a portion of the saturated steam produced downstream in the process in line 25.

The hot raw gas stream containing residue from the partial oxidation reaction i.e. entrained particulate solids and molten slag leaves reaction zone 2, passes downwardly through connecting passage 5 at high velocity, and enters gas diversion chamber 4 where the velocity of the gas stream is suddenly reduced. About 45 to 50 wt. % of the entrained solids and slag drop out of the gas stream by gravity in diversion chamber 4 and pass through outlet 30 in the bottom of diversion chamber 4. The central vertical longitudinal axes of passage 5 and outlet 30 lie along the central longitudinal vertical axis of vessel 1. The solid material and slag drop into water 31 contained in slag chamber 6 at the bottom of vessel 1. In order to keep outlet 30 clear and free from solid material, a portion i.e. about 1 vol. % of the gas stream is diverted through bottom outlet 30 and refractory lined outlet 32 in the side wall of vessel 1 above the level of water 31 in the bottom. As previously described the bleed gas is passed through insulated line 33, water cooled valve 34, insulated line 17 and into heat exchanger 16. A mixture of hot water and solids is removed from the bottom of vessel 1 through bottom outlet 8, lines 35, 36, heat exchanger 37, line 38, valve 39, and line 40 to a lockhopper system (not shown). Solids are removed from the quench water in a solids recovery zone (not shown), and the quench water is returned to slag chamber 6 by way of line 41 and side inlet 42.

When bridging of bottom outlet 30 is not a problem, then all of the hot raw gas stream entering gas diversion chamber 4 exits by way of side outlet 43. From there the hot gas stream passes through transfer line 44 at a high velocity. Transfer line 44, is a passageway lined with refractory 45. The gas stream enters the second gas diversion and residue separation chamber 46 located in second pressure vessel 50 by way of inlet 47. By inclining transfer line 44, for example, about 60° measured clockwise from the vertical central axis of vessel 50 starting from the third quadrant, as shown in the drawing, molten slag that separates from the gas stream may easily run down the transfer line and flow back into gas diversion chamber 4. From there the slag drops into the pool of water at the bottom of slag chamber 6. The design of the second gas diversion and residue separation chamber 46 in pressure vessel 50 is similar to that previously described for the first gas diversion and residue separation chamber 4 in the first pressure vessel. However, the size of gas diversion chamber 46 is larger than that of gas diversion chamber 4. This will provide the gas stream passing upwardly through gas diversion chamber 46 with a longer dwell time for separation of particulate matter and slag. About 25 to 30 wt. % of the total amount of particulate matter and slag is removed from the gas stream in the second gas diversion chamber 46. Gas diversion and solid separation chamber 46 is equipped with upper outlet 48 and bottom outlet 49. The central vertical longitudinal axes of outlets 48 and 49 lie along the central vertical longitudinal axis of closed vertical cylindrical pressure vessel 50. Gas diversion chambers 4 and 46 are either made from a thermal refractory material 51, or they are lined with a thermal refractory material. By this means, there is substantially no drop in temperature or pressure as the gas stream passes through free-flow diversion chambers 4 and 46. Solid material and slag which separate by gravity from the gas stream in diversion chamber 46, drop through bottom outlet 49 into a pool of water 52 located in the second slag chamber 53 at the bottom of vessel 50. When necessary, for example with high slagging feedstocks, a very small portion of the hot raw gas stream passing through diversion chamber 46 is continuously passed through bottom outlet 49, refractory lined side outlet 54 located at the bottom of vessel 50 and above the level of water pool 52, insulated line 55, water cooled valve 56 and insulated line 18. Optionally, the bleed gas in line 18 may be mixed with the bleed gas in line 17 and used to preheat the coal-water slurry in heat exchanger 16. Alternatively, the bleed gas in line 18 may be mixed downstream with most of the gas stream leaving a convection type gas cooler (not shown). The hot water containing solids in water pool 52 leaves by way of central outlet 57 at the bottom of vessel 50, and line 58. Advantageously, the sensible heat in this stream of water is recovered by mixing it with the water containing solids in line 35 from vessel 1 and passing the mixture through line 36 into heat exchanger 37.

The hot raw gas stream passing upwardly through gas diversion solid separation chamber 46, leaves by way of upper central outlet 48 and enters directly into the bottom of radiant cooling section 65. This section comprises a radiant boiler and is located in the upper portion of vessel 50. Tube wall 66, through which a coolant flows, is part of the radiant boiler and lines the inside walls of the upper section of vessel 50. The gas-tight tube wall protects the inside surfaces of the steel pressure vessel from corrosive and thermal damage from the hot gas stream that contacts the outside surfaces of the tubes while passing upwardly through the radiant cooling section. Tube wall 66 is in communication with annular header 67 at the bottom and annular header 68 at the top. By this means the coolant enters bottom header 67 by way of line 69 and inlet 70, passes upwardly through the individual upright tubes in tube wall 66 to upper header 68, and leaves by outlet 71 and line 72. Tube wall 66 may comprise a plurality of vertical thin-walled tubes that are longitudinally welded to each other. The velocity of the hot raw gas stream passing up through the radiation section 65 is less than that of the gas stream passing up through diversion chamber 46; which velocity in turn is less than the velocity of the gas stream passing down through gas diversion chamber 4. Similarly, the dwell time of the gas stream in radiant cooling section 65 is greater than that in gas diversion chamber 46; which dwell time in turn is greater than that in gas diversion chamber 4. There are no obstructions along the central longitudinal vertical cylindrical shaped core of radiant boiler 65. Accordingly, the upflowing hot raw gas stream passes freely therethrough; and, about 10 to 15 wt. % of the total solids produced in the gas generator drop out of the gas stream and fall down by gravity through openings 48 and 49 into the pool of quench water 52. Tube-wall 66 encircles said central passage.

Makeup quench water may be introduced into slag chamber 53 by way of line 75 and inlet 76 at the bottom of vessel 50. Slag chambers 6 and 53 may be water jacketed or insulated. Annular shaped water jackets 120 and 121, respectively line the inside walls of slag chambers 6 and 53. Cooling water enters said cooling jackets by way of lines 123 to 125 and inlets 126 and 127. Heated water leaves jacket 120 through upper outlet 128 and line 129. Heated water leaves jacket 121 through upper outlet 130 and line 131.

In a preferred embodiment, makeup boiler feed water (BFW) in line 77 is preheated in heat exchanger 37 by indirect heat exchange with one or both of the hot water streams containing solid material from slag chambers 6 and 53. The preheated BFW is passed through line 78 and mixed in line 69 with water from line 79. The preheated water in line 69 is passed through inlet 70 into lower header 67. The water rises in tube wall 66 and is heated by indirect heat exchange with the hot gas stream flowing upwardly through the radiant cooling section. A mixture of water at its boiling point and steam leaves upper header 68 through outlet 71, line 72, and enters steam drum 85. The steam and water separate in steam drum 85 and water is removed by way of bottom outlet 86 and line 79. The water is recycled to the lower header 67 of radiant boiler 65 as previously described. Saturated steam is removed from steam drum 85 by way of upper outlet 87, line 88, valve 89 and line 25. This saturated steam may be used elsewhere in the process thereby increasing the thermal efficiency of the process. For example, the saturated steam may be superheated and used as the working fluid in a steam turbine for the production of mechanical power, or electrical energy, or both.

The partially cooled and cleaned gas leaves the radiant cooling section 65 by way of outlet 90 at or near the top of vessel 50. Outlet 90 is connected directly to an energy utilizing device (not shown) which operates downstream at elevated pressure. The connection may be at an angle, for example, of 0° to 90° with the vertical axis of vessel 50. By this means, the energy utilizing device may be operated at the same pressure as the gas produced in gas generator 3 less ordinary pressure drop in the lines. Advantageously, by the subject invention the temperature of the gas stream may be reduced in radiant cooling section 65 to below the maximum safe operating temperature of the downstream energy utilizing means. Further, by removing from about 70 to 95 wt. % of the entrained solids and slag from the hot raw gas stream by means of the subject process, the life and performance of said energy utilizing means is increased. For example, the partially cooled and cleaned gas stream from outlet 90 may be introduced directly into a conventional convection type gas cooler thereby superheating and/or generating steam and heating boiler feed water. Thence, the gas, still substantially at generation pressure may be further scrubbed of particulate matter by well known systems. See coassigned U.S. Pat. No. 3,097,081 for further processing of the gas stream to produce a clean chemical synthesis feed stream or for use as a clean fuel gas. Alternately, the partially cooled and cleaned gas stream leaving outlet 90 may be introduced directly as the working fluid into an expansion turbine for the production of mechanical power, electrical energy, or both.

As previously described, closed vertical steel pressure vessel 50 comprises three principal sections which are connected and communicating: (1) radiant cooling section 65, (2) gas diversion and residue separation section 46, and (3) slag cooling and removal section 53. Optionally, these three sections may be contained in one or more separate pressure vessels which are assembled vertically and interconnected in the order shown in the drawing.

FIG. 2 is a cutaway diagramatic representation of one embodiment of the invention in which the gas diversion and solids separation chamber 46 (of FIG. 1) in the second pressure vessel 50 is replaced by a cyclone separator 100. Reference numbers in FIG. 2 which are the same as the corresponding reference numbers in FIG. 1, have been described previously in connection with FIG. 1. Cyclone 100 is supported in the second pressure vessel 50 by conventional means (not shown), such as brackets. Cyclone 100 is located below the radiant cooling section 65 and above the second slag chamber 53. Thermal insulation 102 on the outside surfaces of cyclone 100 prevents the loss of heat from the hot raw gas stream passing through the cyclone. Annular passage 103 between the outside diameter of the insulated cyclone and the inside diameter of the tube wall permits any falling solid matter and slag from above to reach second slag chamber 53 below. Cyclone 100 is essentially a settling chamber in which the force of gravity is replaced by centrifugal acceleration. The hot raw gas stream leaving the first gas diversion and solids separation chamber 4 in FIG. 1, passes through insulated transfer line 45, and enters cyclone 100 by way of tangential inlet 104. The path of the hot gas stream inside the cyclone involves a double vortex with the hot raw gas stream spiraling downward at the outside and the clean gas stream spiraling upward on the inside to outlet 105 at the top. The clean gas stream leaves the cyclone by way of upper outlet 105, directly enters into the bottom of radiant cooling section 65 and passes upwardly therethrough in indirect heat exchange with the coolant in tube-wall 66, and leaves through upper outlet 90 (shown in FIG. 1). The solid particles entrained in the gas stream entering the cyclone, by virtue of their inertia, will tend to move in the cyclone toward the separator wall from which they are led through annular passage 106 into dust trap 107 located below vortex shield 108. Small size particles will form clusters that may be easily removed from the cyclone by way of bottom outlet 109. The solid matter drops into the pool of quench water 52 contained in the bottom of slag chamber 53. The steps of removing the mixture of quench water and solids by way of bottom outlet 57 and line 58; heat exchange; recovery of quench water in a solids removal zone (not shown); and recycle of the quench water back to the slag chamber 53 by way of line 75 and inlet 76 are the same as that described previously in connection with FIG. 1. In another embodiment, bridging of bottom outlet 109 is prevented by passing through said outlet, a small hot stream of bleed gas taken from the main gas stream in transfer line 44 by way of insulated line 110, cooled valve 111, and insulated line 112. As described in connection with FIG. 1, the bleed gas is discharged from slag chamber 53 by way of refractory lined side outlet 54, insulated line 55, water cooled valve 56 and insulated line 18. The bleed gas may be used to preheat the coal-water slurry. Subsequently, the bleed gas stream is mixed with the main gas stream, and optionally if necessary, the mixture is subjected to additional scrubbing downstream in the process.

One single stage cyclone is shown in FIG. 2 with its longitudinal vertical central axis coaxial with the longitudinal vertical central axis of pressure vessel 50. In another embodiment, where space permits, a plurality of single stage cyclones, which optionally discharge into a common plenum chamber may be employed. In another embodiment, at least one multiple-stage cyclone is employed and the partially cleaned gas stream that is discharged from a first-stage cyclone is passed into the inlet of a second-stage cyclone. The clean gas stream from each second-stage cyclone may be discharged into the radiant cooling section 65 or into a common plenum chamber which discharges into the radiant cooling section. In still other embodiments, a conventional impingement separator may be used instead of a cyclone to replace the second gas diversion and solid separation chamber in second pressure vessel 50.

Other modifications and variations of the invention as hereinbefore set forth may be made without departing from the spirit and scope thereof, and therefore only such limitations should be imposed on the invention as are indicated in the appended claims. 

We claim:
 1. A process for separating entrained solid matter and slag from a hot raw gas stream comprising H₂, CO, CO₂, entrained solid matter and slag, and one or more materials from the group H₂ O, H₂ S, COS, CH₄, NH₃, N₂, and A as produced in the reaction zone of a gas generator by the partial oxidation of solid carbonaceous fuel at a temperature in the range of about 1800° to 3000° F. and a pressure in the range of about 10 to 190 atmospheres, and cooling said hot raw gas stream comprising:(1) passing said hot raw gas stream directly from said reaction zone downard through a connecting passage at high velocity into a first thermally insulated unobstructed free-flow gas diversion and residue separation chamber where the velocity of the gas stream is reduced, said first residue separation chamber having a net internal volume which is smaller than than that of said reaction zone and having bottom and side outlets, separating by gravity a portion of said solid matter and slag from the gas stream without substantially reducing the temperature of the gas stream, and passing said portion of separated material by gravity through said bottom outlet into a first slag pot located directly below said first gas diversion and residue separation chamber; (2) passing about 80.0 to 100 vol. % of the hot gas stream from said first gas diversion and residue separation chamber with a portion of said solid matter and slag removed through said side outlet and then through a thermally insulated transfer line directly into a second thermally insulated unobstructed freeflow gas diversion and residue separation chamber where the velocity of the gas stream is changed, the second gas diversion and residue separation means being sized larger than said first gas diversion and residue separation chamber and having bottom and top outlets and being located in a separate vertical pressure vessel from that containing said first gas diversion and residue separation chamber, separating additional solid matter and slag from the gas stream by gravity without substantially reducing the temperature of the gas stream, and passing said separated portion of material into a second slag pot located directly below said second gas diversion and residue separation chamber; (3) passing about 80.0 to 100 vol. % of the hot gas stream from said second gas diversion and residue separation chamber with a portion of said solid matter and slag removed upward through said top outlet and directly into the bottom of and upward through the unobstructed central vertical passage of a radiant cooling zone at a reduced velocity simultaneously cooling said gas stream and removing additional solid matter and slag from said gas stream, by gravity, and passing said separated portion of material into said second slag pot; and (4) removing a cleaned gas stream from said radiant cooling zone at a reduced temperature.
 2. The process of claim 1 provided with the step of quench cooling said separated portion of solid matter and slag in quench water contained in the bottom of either one or both of said slag pots, producing hot quench water containing solid matter and slag.
 3. The process of claim 2 provided with the steps of passing said hot quench water containing solid matter and slag in indirect heat exchange with boiler feed water thereby preheating said boiler feed water, and introducing said preheated boiler feed water into the radiant cooling section as a portion of the coolant.
 4. The process of claim 3 provided with the step of passing said preheated boiler feed water upwardly through a tube wall in said radiant cooling section.
 5. The process of claim 2 provided with the steps of simultaneously passing a bleed gas stream of about 0.5 to 20 vol. % of the hot gas stream entering said first, second, or both gas diversion and residue separation chambers into said quench water and removing the bleed gas stream from said slag pots.
 6. The process of claim 1 wherein the second gas diversion and residue separation means in step (2) is a single-stage cyclone.
 7. The process of claim 1 provided with the step of introducing the hot raw gas stream into the second gas diversion and residue separation chamber by way of a transfer line whose longitudinal central axis makes an angle with the central vertical axis of the second gas diversion and solids separation chamber in the range of about 30° to 120° measured clockwise starting in the third quadrant.
 8. The process of claim 1 wherein the net internal volumetric ratio of the radiant cooling zone to the reaction zone in the gas generator is in the range of about 5 to
 10. 9. The process of claim 1 wherein the net internal volumetric ratio of the second to the first gas diversion and residue separation chamber is in the range of about 4 to
 10. 10. The process of claim 1 wherein the net internal volumetric ratio of the gas generator reaction zone to the first gas diversion and residue separation chamber is in the range of about 2 to
 20. 11. The process of claim 1 wherein said solid carbonaceous fuel is selected from the group consisting of particulate carbon, coal, coke from coal, lignite, petroleum coke, oil shale, tar sands, asphalt, pitch, and mixtures thereof.
 12. The process of claim 1 wherein said solid carbonaceous fuel is subjected to partial oxidation either alone or in the presence of substantially thermally liquifiable or vaporizable hydrocarbon or carbonaceous materials and/or water.
 13. The process of claim 1 wherein said solid carbonaceous fuel is introduced into the gas generator entrained in a gaseous medium from the group consisting of steam, CO₂, nitrogen, synthesis gas, and air.
 14. The process of claim 1 wherein a free-oxygen containing gas selected from the group consisting of air, substantially pure oxygen, and mixtures thereof is employed in said partial oxidation process.
 15. The process of claim 1 provided with the step of introducing at least a portion of the cleaned and cooled gas stream from step 4 directly into an energy utilizing zone.
 16. The process of claim 15 wherein said energy utilizing zone comprises a convection-type gas cooler.
 17. The process of claim 15 wherein said energy utilizing zone comprises an expansion turbine for the producton of mechanical energy, electrical energy, or both.
 18. The process of claim 1 with the step of passing said hot gas stream from said first gas diversion and residue separation chamber in step (2) into said second gas diversion and residue separation chamber by way of an upwardly or downwardly directed transfer line.
 19. The process of claim 1 with the step of passing about 0.5 to 20 vol. % of the hot gas stream entering said first, second, or both gas diversion and residue separation chambers respectively through said bottom outlets to prevent bridging.
 20. The process of claim 1 provided with the step of cooling the hot gas stream passing upwardly through the central passage of the radiant cooling zone in step (3) by indirect heat exchange with boiler feed water passing upward through a vertical tube-wall encircling said passage.
 21. A process for separating entrained solid matter and slag from a hot raw gas stream comprising H₂, CO, CO₂, entrained solid matter and slag, and one or more materials from the group H₂ O, H₂ S, COS, CH₄, NH₃, N₂, and A as produced in the reaction zone of a gas generator by the partial oxidation of solid carbonaceous fuel at a temperature in the range of about 1800° to 3000° F. and a pressure in the range of 10 to 190 atmospheres, and cooling said hot raw gas stream comprising:(1) passing said hot raw gas stream directly from said reaction zone downward through a connecting passage at high velocity into a thermally insulated unobstructed free-flow gas diversion and residue separation chamber where the velocity of the gas stream is reduced, said residue separation chamber having a net internal volume which is smaller than that of said reaction zone and having bottom and side outlets, separating by gravity a portion of said solid matter and slag from the gas stream without substantially reducing the temperature of the gas stream, and passing said portion of separated material by gravity through said bottom outlet into a first slag pot located directly below said first gas diversion and residue separation chamber; (2) passing about 80.0 to 100 vol. % of the hot gas stream from said first gas diversion and residue separation chamber with a portion of said solid matter and slag removed through said side outlet and then through a thermally insulated transfer line directly into a thermally insulated cyclone means located in a separate vertical pressure vessel from that containing said gas diversion and residue separation chamber and having lower and upper outlets, separating additional solid matter and slag from the gas stream by said cyclone means without substantially reducing the temperature of the gas stream, and passing said separated portion of material through said lower outlet into a second slag pot located directly below said cyclone means; (3) passing about 80.0 to 100 vol. % of the hot gas stream with a portion of said solid matter and slag removed upward through the upper outlet in said cyclone means and direct into the bottom of and upward at a reduced velocity through the unobstructed central vertical passage of a radiant cooling zone having a plurality of vertical tubes lining on the inside walls, simultaneously cooling said upflowing hot gas stream to below the maximum safe operating temperature for a downstream energy utilizing means by indirect heat exchange with water flowing in said vertical tubes to produce by-product steam and solidifying at least the outer shell of any remaining ash particles in the gas stream, and removing additional solid matter and slag from said gas stream by gravity, and passing said separated portion of material into said second slag pot; and (4) removing a cleaned gas stream from said radiant cooling zone at a reduced temperature.
 22. The process of claim 21 wherein said cyclone means is a single-type cyclone.
 23. The process of claim 21 provided with the steps of quench cooling said separated portion of solid matter and slag in quench water contained in the bottom of either one or both of said slag pots, producing hot quench water containing solid matter and slag.
 24. The process of claim 21 provided with the steps of either (1) passing a stream of bleed gas comprising about 0.5 to 20 vol. % of the hot gas stream from said reaction zone into either said first slag pot along with said separated solid matter and slag, or (2) passing a stream of bleed gas comprising about 0.5 to 20 vol. % of the hot gas stream from said transfer line through said lower outlet of said cyclone means into said second slag pot thereby preventing bridging of said bottom outlet; or passing a stream of bleed gas in accordance with both (1) and (2); and removing said bleed gas from said slag pots.
 25. The process of claim 21 where in step (2) said hot gas stream from step (1) is introduced into said cyclone means by way of a thermally insulated transfer line whose longitudinal central axis makes an angle with the central vertical axis of said separate vertical pressure vessel in the range of about 30° to 120° measured clockwise starting in the third quadrant. 